CN205933756U - System for lighter hydrocarbons are stabilized to isothermal division A league matches of french football mellow wine conversion system - Google Patents

Abstract

The utility model relates to a system for lighter hydrocarbons are stabilized to isothermal division A league matches of french football mellow wine conversion system, a serial communication port, the system includes the raw material methanol feeding mechanism, methyl alcohol gasification over heater, the reactor, steam generator, cooler and oily deareator, the raw material input mouth of exit linkage to the methyl alcohol gasification over heater of raw material methanol feeding mechanism, the raw materials delivery outlet of methyl alcohol gasification over heater is connected to the reaction material import of reactor, the reaction material of reactor is connected to steam generator's hot material import, the heat recovery import of steam generator's hot material exit linkage to methyl alcohol gasification over heater, the hot recovery outlet of methyl alcohol gasification over heater is connected to the cooler, cooler and oily deareator intercommunication. The utility model discloses need not to set up recycle gas compressor and circulating air heat exchanger, have characteristics such as process flow is simple, equipment is small in quantity, the investment economizes, the flow energy consumption is low, product yield height.

Description

A kind of isothermal method methanol converts the system of stable light hydrocarbon processed

Technical field

This utility model is related to methanol conversion technique for preparing gasoline field, in particular to a kind of conversion of isothermal method methanol The system of stable light hydrocarbon processed.

Background technology

China belongs to the country of petroleum resources critical shortage, growing continuously and fast recently as Chinese national economy, Energy demand is continuously increased, and petroleum import interdependency increases year by year.And coal in China reserves very abundant, thus determine China Must greatly develop with coal clean conversion using the Coal Energy Source Chemical Engineering Technology being characterized.The more maturation of coal conversion at present One of technique is methanol-fueled CLC, and also just because of this, China's methanol production scale constantly expands, and has gradually formed methanol production capacity surplus And others Coal Chemical Industry Route situation hard to carry on, therefore, greatly develop methanol downstream technique, produce first using synthesis gas The large energy products of catalyzed conversion production have become the important development direction that China develops derived energy chemical again for alcohol, methanol.

The methanol that it is that Mobil company developed the seventies in last century that methanol converts stable light hydrocarbon technology processed utilizes technique road Line.This technology is using ZSM-5 type synthetic zeolite catalyst, methanol dehydration to be converted into main component to concentrate on C₅～C₁₀Between Hydrocarbon mixture, thus the method producing high-knock rating gasoline.

The reaction that stable light hydrocarbon is produced in methanol conversion belongs to strong exothermal reaction, at 400 DEG C, often conversion 1kg methanol release Reaction heat be 1.74MJ, under conditions of not having heat exchange and dilution, adiabatic temperature rise is more than 600 DEG C.Therefore must be using suitably Technique will react release amount of heat removal reactor, so that temperature of reactor is controlled.

United States Patent (USP) US3931349 discloses Mobil company two-step method methanol synthesized gasoline technique.This technique first step is Methanol dehydration generates dimethyl ether, and second step is dimethyl ether and unreacted methanol is catalyzed by ZSM-5 molecular sieve in reactor Agent is converted into hydrocarbon mixture.This technique adopts the method that residue gas recycle reduces adiabatic temperature rise, to realize the temperature to course of reaction Degree controls, and is to control within 120 DEG C by adiabatic temperature rise, the volume ratio of circulation dry gas and methanol steam is at least more than 5.The party The circulating device circulating consumption that method process is complicated, be related to is high, and equipment is had high demands, and production cost is high.

Chinese patent ZL200610048298.9 discloses the technique that a kind of methanol by one-step method produces hydrocarbon productss, this patent Introduce fixed bed adiabatic reactor, one-step synthesis method gasoline products using by material benzenemethanol, eliminate methanol preparation of dimethyl ether step Suddenly, flow process is simple.But methanol liberated heat in conversion process is more, substantial amounts of recyclegas is needed to take away heat of reaction, The recycle stock of this patent requirements and the mass ratio of methanol feedstock are 10-20, and circulating consumption is high, recycle compressor cost is expensive.

Further, Chinese patent CN 105419849A is directed to, circulating flow rate present in above-mentioned technique is big, recycle unit investment A kind of high the shortcomings of, there is provided the technique that energy-saving methanol converts gasoline processed.This patent is provided with before MTG synthesis reactor Two-stage pre-reactor, will gasification overheated after methanol carry out pre-reaction in the first pre-reactor, carry out in the second pre-reactor Reaction, the reaction gas outlet of the second pre-reactor enters artificial oil from top after mixing with the circulating air from recycle gas compressor Reacted in reactor.Although this patent overcomes in aforementioned two-step method and one-step method MTG technique to a certain extent existing The defect that circulating flow rate is big, recycle unit investment is high, reduce energy consumption and production cost, but the production technology of this patent be still So cannot avoid using recycle gas compressor, and the mass ratio of the gas outlet of circulating air and the second pre-reactor is 2-4, it is simultaneously Input on recycle gas compressor is not completely eliminated.

Utility model content

The purpose of this utility model is the system providing a kind of isothermal method methanol to convert stable light hydrocarbon processed, and it need not be arranged Recycle gas compressor and circulating air heat exchanger, have that technological process is simple, number of devices is few, reduced investment, flow process energy consumption are low, product The advantages of high income.

For achieving the above object, this utility model spy employs the following technical solutions：

A kind of isothermal method methanol converts the system of stable light hydrocarbon processed, and system includes material benzenemethanol feeding mechanism, methanol gasifying Superheater, reactor, steam generator, cooler and oil gas water separator, the outlet of material benzenemethanol feeding mechanism connect to The feedstock input of methanol gasifying superheater, the raw material delivery outlet of methanol gasifying superheater connects to enter to the reaction mass of reactor Mouthful, the reacting material outlet of reactor connects to the thermal material import of steam generator, and the material outlet of steam generator is even It is connected to the recuperation of heat import of methanol gasifying superheater, the recuperation of heat outlet of methanol gasifying superheater connects to cooler, cooler Connect with oil gas water separator.

In this utility model preferred embodiment, above-mentioned methanol gasifying superheater includes the methanol gasifying device being independently arranged With methanol superheater, material benzenemethanol inflow methanol superheater, raw material delivery outlet and the recuperation of heat after methanol gasifying device is processed Import is respectively arranged on methanol superheater, and feedstock input and recuperation of heat outlet are arranged on methanol gasifying device.

In this utility model preferred embodiment, above-mentioned reactor includes the thermal insulation communicating with each other and arranging independently of one another Pre-reactor and isothermal reactor, the first material import of adiabatic pre-reactor connects to the raw material output of methanol gasifying superheater Mouthful, the first material outlet of isothermal reactor connects to the thermal material import of steam generator.

In this utility model preferred embodiment, above-mentioned reactor includes the isothermal communicating with each other and arranging independently of one another Pre-reactor and isothermal main reactor, the second material import of isothermal pre-reactor connects defeated to the raw material of methanol gasifying superheater Outlet, the second material outlet of isothermal main reactor connects to the thermal material import of steam generator.

In this utility model preferred embodiment, the isothermal that above-mentioned reactor is included for carrying out isothermal pre-reaction section is pre- Reative cell and the isothermal main reaction chamber for carrying out isothermal primary response section, isothermal pre-reaction room and isothermal main reaction chamber are respectively provided with In the inside of reactor and communicate with each other, the reacting material inlet of reactor is connected with isothermal pre-reaction room, reactor anti- Material outlet is answered to be connected with isothermal main reaction chamber.

In this utility model preferred embodiment, above-mentioned reactor includes the adiabatic pre-reaction being arranged on inside reactor Room and isothermal reaction room, and adiabatic pre-reaction room communicates with each other with isothermal reaction room, the reacting material inlet of reactor with exhausted Hot pre-reaction room connects, and the reacting material outlet of reactor is connected with isothermal reaction room.

In this utility model preferred embodiment, above-mentioned reactor is isothermal reactor, and isothermal reactor includes being catalyzed Agent bed side and cooling medium side.

In this utility model preferred embodiment, said system also includes cooling medium circulation device, and cooling medium follows Loop device is connected with the cooling medium side of isothermal reactor.

Advantageous Effects of the present utility model：

(1) system structure of isothermal method conversion stable light hydrocarbon processed of the present utility model is simple, used device is few, reduced investment. Compare and convert the device major part of stable light hydrocarbon processed all using the detached gas phase of oil gas water separator as following with existing methanol For ring gas control alkylation reaction temperature, system of the present utility model adopts isothermal reactor, and reaction temperature is controlled all the time In the range of one stationary temperature, directly eliminate the recycle gas compressor in existing preparation system and circulating air heat exchanger, if Standby investment saving 30%～50%.

(2) the flow process energy consumption of system of the present utility model is low, by arranging adiabatic pre-reactor before reactor, or Adiabatic pre-reaction room is set in reactor so that material benzenemethanol first carried out pre-reaction preheating before carrying out alkylation reaction, leads to The heat of reaction crossing the acquisition of pre-reaction autoreactivity makes material naturally reach reaction temperature close to alkylation reaction, pre- anti-to reduce Answer early stage required heat overheated to methanol.Simultaneously as system need not arrange circulating air, it is to avoid because of circulating air plus hot and cold But the consumption to System steam and cooling water.System of the present utility model does not only need to consume steam, but also can be with by-product High steam, also reduces circulating cooling water consumption (the circulating cooling water consumption that system of the present utility model uses simultaneously For existing apparatus 10%～50%), operation energy consumption is low.

Brief description

In order to be illustrated more clearly that the technical scheme of this utility model embodiment, below will be to use required in embodiment Accompanying drawing be briefly described it will be appreciated that the following drawings illustrate only some embodiments of the present utility model, therefore should be by Regard the restriction to scope as, for those of ordinary skill in the art, on the premise of not paying creative work, also may be used To obtain other related accompanying drawings according to these accompanying drawings.

Fig. 1 is the structure chart of the system of isothermal method methanol conversion stable light hydrocarbon processed of this utility model embodiment 1；

Fig. 2 is the structure chart of the system of isothermal method methanol conversion stable light hydrocarbon processed of this utility model embodiment 2；

Fig. 3 is the structure chart of the system of isothermal method methanol conversion stable light hydrocarbon processed of this utility model embodiment 3；

Fig. 4 is the structure chart of the system of isothermal method methanol conversion stable light hydrocarbon processed of this utility model embodiment 4；

Fig. 5 is the structure chart of the system of isothermal method methanol conversion stable light hydrocarbon processed of this utility model embodiment 5.

Reference numerals list：

Isothermal method methanol converts the system 100,200,300,400,500 of stable light hydrocarbon processed；Methanol gasifying superheater 110； Reactor 120；Steam generator 130；Cooler 140；Oil gas water separator 150；Drum 160；Material benzenemethanol feeding mechanism 170；Cooling water make-up pump 180；Raw material delivery outlet 111；Recuperation of heat import 112；Recuperation of heat outlet 113；Feedstock input 114； Reacting material inlet 121；Reacting material outlet 122；Thermal material import 131；Material outlet 132；High-pressure cold water S11；Steam Mixture S12；Saturation water S13；High steam S14；Cool circulation water S15；Heat recirculated water S16；

Methanol gasifying device 210；Methanol superheater 220；Adiabatic pre-reactor 230；Isothermal reactor 240；Raw material delivery outlet 211；Recuperation of heat import 212；Recuperation of heat outlet 213；Feedstock input 214；First material import 231；First material exports 241；Low temperature conduction oil S27；High temperature heat conductive oil S28；

Isothermal pre-reactor 320；Isothermal main reactor 330；Second material import 321；Second material outlet 331；Pre- anti- Answer section low temperature conduction oil S39；Pre-reaction section high temperature heat conductive oil S40；

Reactor 420；Isothermal pre-reaction room 421；Isothermal main reaction chamber 422；Reacting material inlet 423；Reaction mass goes out Mouth 424；Primary response section low temperature conduction oil S47；Primary response section high temperature heat conductive oil S48；Pre-reaction section low temperature conduction oil S49；Pre- anti- Answer section high temperature heat conductive oil S50；

Reactor 520；Adiabatic pre-reaction room 521；Isothermal reaction room 522；Reacting material inlet 523；Reacting material outlet 524；Primary response section low temperature conduction oil S57；Primary response section high temperature heat conductive oil S58.

Specific embodiment

Below in conjunction with embodiment, embodiment of the present utility model is described in detail, but those skilled in the art It will be understood that, the following example is merely to illustrate this utility model, and is not construed as limiting scope of the present utility model.Embodiment In unreceipted actual conditions person, according to normal condition or manufacturer suggestion condition carry out.Agents useful for same or the unreceipted life of instrument Produce manufacturer person, being can be by the commercially available conventional products bought and obtain.

It should be noted that：Similar label and letter represent similar terms in following accompanying drawing, therefore, once a certain Xiang Yi It is defined in individual accompanying drawing, then do not need it to be defined further and explains in subsequent accompanying drawing.

In addition it is also necessary to explanation in description of the present utility model, unless otherwise clearly defined and limited, term " sets Put ", should be interpreted broadly " installation ", " being connected ", " connection ", for example, it may be being fixedly connected or being detachably connected, Or be integrally connected；Can be to be mechanically connected or electrically connect；Can be to be joined directly together it is also possible to pass through intermediary It is indirectly connected to, can be the connection of two element internals.For the ordinary skill in the art, can be managed with concrete condition Solve concrete meaning in this utility model for the above-mentioned term.

With reference to embodiment, this utility model is further illustrated.

Embodiment 1

Referring to Fig. 1, the system 100 that isothermal method methanol converts stable light hydrocarbon processed includes：Material benzenemethanol feeding mechanism 170, first Alcohol gasification superheater 110, reactor 120, steam generator 130, cooler 140 and oil gas water separator 150.As Fig. 1 institute Show, according to the flow direction of reaction mass (that is, material benzenemethanol), the outlet of material benzenemethanol feeding mechanism 170 connects to methanol gas Change the feedstock input 114 of superheater 110.The raw material delivery outlet 111 of methanol gasifying superheater 110 connects to reactor 120 Reacting material inlet 121.The reacting material outlet 122 of reactor 120 connects to the thermal material import 131 of steam generator 130. The material outlet 132 of steam generator 130 connects to the recuperation of heat import 112 of methanol gasifying superheater 110.Methanol gasifying mistake The recuperation of heat outlet 113 of hot device 110 connects to cooler 140.Cooler 140 is connected with oil gas water separator 150.

The outlet of material benzenemethanol feeding mechanism 170 is connected with the feedstock input 114 of methanol gasifying superheater 110.Raw material Methanol feeding mechanism 170 includes methanol tank (not shown) and the methanol transport pump (not shown) being connected with methanol tank, leads to Cross the liquid material methanol that methanol transport pump conveys certain pressure to methanol gasifying superheater 110.

Methanol gasifying superheater 110 is used for the material benzenemethanol of liquid being gasified and being carried out Overheating Treatment, is allowed to convert For gaseous state and be heated to the required temperature of reaction.Methanol gasifying superheater 110 includes feedstock input 114, raw material delivery outlet 111st, recuperation of heat import 112 and recuperation of heat outlet 113.Wherein, the feedstock input 114 of methanol gasifying superheater 110 with former The outlet of material methanol feeding mechanism 170 connects, for introducing material benzenemethanol.The raw material delivery outlet 111 of methanol gasifying superheater 110 Connect to the reacting material inlet 121 of reactor 120.The recuperation of heat import 112 of methanol gasifying superheater 110 connects to be sent out to steam The material outlet 132 of raw device 130, thus reclaiming the heat of the material after processing through steam generator 130 recuperation of heat further, This partial heat reclaiming is used for the material benzenemethanol in heating methanol gasification superheater 110.The heat of methanol gasifying superheater 110 Reclaim outlet 113 to connect to cooler 140, the material after recuperation of heat twice is processed is passed through in cooler 140 and carries out Next step cooling treatment.

Reactor 120 is the isothermal reactor converting stable light hydrocarbon processed for carrying out methanol.E.g., around tubular reactor Or shell and tube reactor.The reacting material outlet 122 of reactor 120 is connected with the thermal material import 131 of steam generator 130. Reactor 120 includes the (not shown) of side containing beds and cooling medium side (not shown).Beds side and cooling are situated between Matter side is spaced apart, does not mutually connect.Wherein, catalyst bed side layer is used for carrying out the alkylation reaction that methanol converts stable light hydrocarbon processed. Cooling medium side is used for being passed through cooling medium and carries out heat exchange, to take away the heat that reaction produces, so that the temperature in reactor is tieed up Hold within the specific limits.The cooling medium side of reactor 120 is connected with cooling medium circulation device.In the present embodiment, cool down Media recycler includes drum 160 and the cooling water make-up pump 180 being connected with drum 160.Specifically, in the present embodiment In, the cooling medium side of reactor 120 is connected with drum 160.Its work process is that drum 160 is passed through height in reactor 120 Pressure cold water S11, after heat exchange, gas-vapor mix S12 of acquisition is returned again in drum 160, carries out steam and separates, produces Raw high steam.Cooling water make-up pump 180 is used for constantly supplementing cooling water in drum 160, persistently to lead to high-pressure cold water S11 Enter and carry out heat exchange to reactor 120, thus the reaction temperature in reactor 120 is maintained a stationary temperature scope Interior.

Steam generator 130 is used for reclaiming the heat of the material after isothermal reaction (that is to say alkylation reaction), to produce High steam.The thermal material import 131 of steam generator 130 is connected with the reacting material outlet 122 of reactor 120.Steam is sent out The material outlet 132 of raw device 130 is connected with the recuperation of heat import 112 of methanol gasifying superheater 110, with further recovered material Heat.The work process of steam generator 130 is will to be sent out with flowing into steam by the saturation water S13 to steam generator 130 Thermal material in raw device carries out heat exchange, produces high steam S14 while reducing thermal material temperature.

Cooler 140 is connected with the recuperation of heat outlet 113 of methanol gasifying superheater 110, for cooling through heat twice Material after recovery.The work process of cooler 140 is, is passed through cool circulation water S15 in cooler 140, cool circulation water S15 with The material flowing in cooler 140 carries out heat exchange, obtains heat recirculated water S16 while reducing temperature of charge, then will Heat recirculated water S16 is used for other work systems, and the cool circulation water S15 obtaining after heat exchange in other work systems is passed through cold again But device 140 carries out heat exchange, so goes round and begins again and carries out heat exchange.In the present embodiment, cooler 140 is water cooler.It is worth saying Bright, in other embodiments, cooler 140 of the present utility model can also be in forced air cooler and heat conduction oil cooler At least one.

Oil gas water separator 150 is connected with cooler 140, for separating material after cooling, be separated into dry gas, Hydrocarbon mixture and fresh water (FW).Wherein, hydrocarbon mixture is the hydrocarbon productss needing preparation.

Below the operation principle of the system 100 that the isothermal method methanol of the present embodiment converts stable light hydrocarbon processed is illustrated.

Material benzenemethanol feeding mechanism 170 is to methanol gasifying superheater 110 transferring raw material methanol.Material benzenemethanol is in methanol gasifying In superheater 110 through gasification, overheated after be passed through to reactor 120, and carry out in the presence of hydrocarbonylation catalyst be dehydrated hydrocarbonylation Reaction.Meanwhile, it is passed through high-pressure cooling water S11 to the cooling medium side in reactor 120, by the gasification of high-pressure cooling water S11 Take away alkylation reaction liberated heat.Gas-vapor mix S12 that cooling medium side is drawn in reactor 120 enters into drum 160 carry out gas-liquid separation, and gas phase is high steam, and liquid phase is saturation water, and wherein, saturation water is back to reactor 120 to be continued to inhale Heat.The material flowing out from the reacting material outlet 122 of reactor 120 sequentially passes through steam generator 130 and methanol gasifying is overheated Device 110 carries out heat recovery.Then, the material after heat recovery is passed through in cooler 140 and cools down further.Finally, cool down Material afterwards enters back into and carries out oil, gas and water three phase separation in oil gas water separator 150.Wherein, separating the oil phase obtaining is C₃~ C₁₀Hydrocarbon mixture, after the lighter hydrocarbons stabilisation systemss simple process of downstream, you can obtain stable light hydrocarbon product (main component be C₅ ～C₁₀).Meanwhile, separating the gas phase obtaining through oil gas water separator 150 is that (main component is C to dry gas₁～C₂), as fuel gas Output device；Separating the aqueous phase obtaining is fresh water (FW), output device.

Embodiment 2

The present embodiment is the improvement further on the basis of embodiment 1, the main distinction of the present embodiment and embodiment 1 It is, the methanol gasifying superheater 110 in embodiment 1 is further separated into the methanol gasifying device arranging independently of one another by the present embodiment 210 and methanol superheater 220, and the reactor 120 in embodiment 1 is divided into the adiabatic pre-reactions of two settings independently of one another Device 230 and isothermal reactor 240.Only the difference part of the present embodiment and embodiment 1 is illustrated below, same section is not Repeat again, it should be appreciated that the present embodiment includes the above-mentioned all technical characteristics not clearly stated in the present embodiment.

Referring to Fig. 2, methanol gasifying device 210 is connected with methanol superheater 220, for the material benzenemethanol of liquid is gasified And carry out Overheating Treatment, make gaseous state and be heated to the required temperature of reaction.After methanol gasifying device 210 is processed Material flows into methanol superheater 220.Methanol gasifying device 210 and methanol superheater 220 are provided separately so that gasifying and superheating process More abundant and easily controllable, fully the carrying out beneficial to subsequent reactions carrying out.Stable light for large-scale methanol conversion system Hydrocarbon device, its effect is especially apparent.And, the present embodiment is also resided in the difference of embodiment 1, and the present embodiment will be arranged on same Feedstock input 114 on equipment (methanol gasifying superheater 110), raw material delivery outlet 111, recuperation of heat import 112 and heat are returned Receive outlet 113 to be provided separately.Thus so that material benzenemethanol is complete with the heat exchange of the thermal material from steam generator 130 Carry out according to reflux type, heat exchange efficiency is higher.Material benzenemethanol feeding mechanism 170 outlet is defeated with the raw material of methanol gasifying device 210 Entrance 214 connects.The raw material delivery outlet 211 of methanol superheater 220 is connected with adiabatic pre-reactor 230, after Overheating Treatment Material benzenemethanol be passed through and carry out pre-reaction to adiabatic pre-reactor 230.Methanol gasifying device 210 recuperation of heat outlet 213 with cold But device 140 connects, and the material after recuperation of heat twice is processed is cooled down further.The recuperation of heat of methanol superheater 220 is entered Mouth 212 is connected with the material outlet 132 of steam generator 130.

The first material import 231 of adiabatic pre-reactor 230 connects to the raw material delivery outlet 211 of methanol superheater.Isothermal The first material outlet 241 of reactor 240 connects to the thermal material import 131 of steam generator 130.

The outlet of the adiabatic pre-reactor 230 being connected with methanol superheater 220 is connected to isothermal reactor 240, for inciting somebody to action Prereacted material after adiabatic pre-reaction section is passed through and carries out alkylation reaction to isothermal reactor 240.In adiabatic pre-reaction In device 230, material benzenemethanol carries out pre-reaction in the presence of pre-reaction catalyst (that is, catalyst for etherification or hydrocarbonylation catalyst). It is not provided with heat-exchanger rig due in adiabatic pre-reactor 230, and external environment near adiabatic, therefore, when carrying out pre-reaction, Prereacted material temperature can be made because substantial amounts of heat is released in reaction to raise, be allowed to close to the reaction temperature entering isothermal reaction section Degree.Reduce overtemperature such that it is able to effective, and then reduce the heat demand of methanol superheater 220 so that more in system Heat is used for byproduct steam, improves steam production.

Isothermal reactor 240 is used for carrying out the alkylation reaction of isothermal reaction section.In isothermal reactor 240, material benzenemethanol Carry out being dehydrated alkylation reaction in the presence of hydrocarbonylation catalyst.Isothermal reactor 240 can be around tubular reactor or shell and tube Reactor.The material outlet of isothermal reactor 240 is connected with the thermal material import 131 of steam generator 130.In the present embodiment In, the cooling medium circulation device being connected with isothermal reactor 240 is conducting oil circulation apparatus (not shown), low temperature conduction oil The import of the cooling medium side from isothermal reactor 240 for the S27 is passed through, and it carries out heat exchange with the material in isothermal reactor 240 Afterwards, obtain high temperature heat conductive oil S28, the then outlet of the cooling medium side from isothermal reactor 240 for the high temperature heat conductive oil S28 is flowed out.

Embodiment 3

The present embodiment is the improvement further on the basis of embodiment 1, the main distinction of the present embodiment and embodiment 1 It is, the reactor 120 in embodiment 1 is divided into the isothermal pre-reactor 320 being independently arranged and isothermal primary response by the present embodiment Device 330.Equally, the present embodiment also only illustrates to difference part, and the same section not clearly stated is also understood to Comprise in the present embodiment.

Referring to Fig. 3, the second material import 321 of isothermal pre-reactor 320 is exported with the raw material of methanol gasifying superheater 110 Mouthfuls 111 connect so that material benzenemethanol after gasification Overheating Treatment in isothermal pre-reactor 320 in pre-reaction catalyst Carry out pre-reaction under effect.In isothermal pre-reaction section, pre-reaction catalyst is catalyst for etherification or hydrocarbonylation catalyst.Isothermal is pre- Reactor 320 is connected with cooling medium circulation device (not shown).In the present embodiment, cooling medium circulation device is conduction oil Circulating device.Conducting oil circulation apparatus are connected with the cooling medium side of isothermal pre-reactor 320, pre-reaction section low temperature conduction oil The import of the cooling medium side from isothermal pre-reactor 320 for the S39 is passed through, and it carries out heat friendship with the material of isothermal pre-reactor 320 After changing, obtain pre-reaction section high temperature heat conductive oil S40, then pre-reaction section high temperature heat conductive oil S40 is cold from isothermal pre-reactor 320 But the outlet of side medium is flowed out.

Isothermal main reactor 330 is used for carrying out the alkylation reaction of isothermal primary response section.In isothermal main reactor 330, warp The material crossing isothermal pre-reaction section continues to carry out alkylation reaction in the presence of hydrocarbonylation catalyst.The of isothermal main reactor 330 Two material outlets 331 are connected with the thermal material import of steam generator 340, by the material after isothermal reaction twice anti- It is passed through to byproduct steam in steam generator 130 after answering completely.Isothermal main reactor 330 is also connected with conducting oil circulation apparatus (not shown).Conducting oil circulation apparatus are connected with the cooling medium side of isothermal main reactor 330, and low temperature conduction oil S27 is from isothermal The import of the cooling medium side of main reactor 330 is passed through, and after its material with isothermal main reactor 330 carries out heat exchange, obtains High temperature heat conductive oil S28, the then outlet of the cooling medium side from isothermal main reactor 330 for the high temperature heat conductive oil S28 is flowed out.

Isothermal pre-reactor 320 and isothermal main reactor 330 are around tubular reactor or shell and tube reactor.In this enforcement In example, by arranging isothermal pre-reactor, material benzenemethanol is carried out in pre-reactor partially dehydrated reaction, effectively reduce isothermal The thermic load of main reactor so that the temperature control of isothermal main reactor more effectively, thus improving reaction selectivity.And, Isothermal reaction is separately positioned in two different isothermal reactors and is reacted, so that reaction is more abundant, simultaneously It is also convenient for overhaul of the equipments and catalyst change.

Embodiment 4

The present embodiment is the improvement further on the basis of embodiment 1, the main distinction of the present embodiment and embodiment 1 It is, the reactor 420 of the present embodiment includes isothermal pre-reaction room 421 and isothermal main reaction chamber 422, by embodiment 1 Isothermal reaction is divided into isothermal pre-reaction section and isothermal primary response section.

Referring to Fig. 4, reactor 420 includes isothermal pre-reaction room 421 and isothermal main reaction chamber 422.Reactor 420 anti- Material inlet 423 is answered to be connected with isothermal pre-reaction room 421.Reacting material outlet 424 and the isothermal main reaction chamber of reactor 420 422 connections.In reactor 420, the material benzenemethanol first pre-reaction catalysis in the isothermal pre-reaction room 421 in reactor 420 Carry out pre-reaction in the presence of agent, then carry out alkylation reaction again in isothermal main reaction chamber 422.Wherein, pre-reaction catalyst For catalyst for etherification.Respectively correspondence is connected with cooling medium circulation device for isothermal pre-reaction room 421 and isothermal main reaction chamber 422 (not shown).In the present embodiment, cooling medium circulation device is conducting oil circulation apparatus.One conducting oil circulation apparatus with etc. Warm pre-reaction room 421 connects, and the import of the cooling medium side from isothermal pre-reaction room 421 for the pre-reaction section low temperature conduction oil S49 is led to Enter, after its material with isothermal pre-reaction room 421 carries out heat exchange, obtain pre-reaction section high temperature heat conductive oil S50, then pre-reaction The outlet of the section cooling medium side from isothermal pre-reaction room 421 for the high temperature heat conductive oil S50 is flowed out.The heat friendship of isothermal main reaction chamber 422 Process of changing is identical with the heat exchanging process of aforementioned isothermal pre-reaction room 421, just repeats no more.In figure, conversion zone low temperature based on S47 Conduction oil, conversion zone high temperature heat conductive oil based on S48.

Reactor 420 is around tubular reactor or shell and tube reactor.The present embodiment passes through setting etc. in reactor 420 Warm pre-reaction section, material benzenemethanol is carried out partially dehydrated reaction in the effect of pre-reaction catalyst, effectively reduces isothermal primary response Section thermic load so that the temperature control of isothermal primary response section more effectively, thus improving reaction selectivity.Simultaneously as will Isothermal pre-reaction section and isothermal primary response section are arranged in same reactor, effectively reduce number of devices, have saved device Take up an area and invest.

Embodiment 5

The present embodiment is the improvement further on the basis of embodiment 1, the main distinction of the present embodiment and embodiment 1 Be, the reactor 520 of the present embodiment includes adiabatic pre-reaction room 521 and isothermal reaction room 522, by embodiment 1 etc. Temperature reaction is divided into adiabatic pre-reaction section and isothermal primary response section.

Referring to Fig. 5, reactor 520 includes adiabatic pre-reaction room 521 and isothermal reaction room 522.The reaction of reactor 520 Material inlet 523 is connected with adiabatic pre-reaction room 521.The reacting material outlet 524 of reactor 520 is with isothermal reaction room 522 even Connect.In reactor 520, the work of the first pre-reaction catalyst in the adiabatic pre-reaction room 521 in reactor 520 of material benzenemethanol With under carry out pre-reaction, then carry out alkylation reaction again in isothermal reaction room 522.Wherein, pre-reaction catalyst is urged for etherificate Agent or hydrocarbonylation catalyst.Isothermal reaction room 522 is connected with cooling medium circulation device (not shown).In the present embodiment, cold But media recycler is conducting oil circulation apparatus.The heat exchanging process of isothermal reaction room 522 and the heat exchange of embodiment 2～4 Process is identical, just repeats no more.In figure, conversion zone low temperature conduction oil based on S57, conversion zone high temperature heat conductive oil based on S58.

Isothermal reaction room 522 in reactor 520 is around tubular type or tubular structure.The present embodiment passes through in reactor In 520, the adiabatic pre-reaction room of setting is to carry out adiabatic pre-reaction so that reaction mass warms naturally to because of adiabatic reaction heat release Temperature needed for isothermal reaction, effectively reduce the load of methanol gasifying superheater so that the heat in system more for by-product High steam, improves steam production.Simultaneously as adiabatic pre-reaction section and isothermal reaction section are arranged at same reactor In, effectively reduce number of devices, save plant area and investment.

The foregoing is only preferred embodiment of the present utility model, be not limited to this utility model, for this For the technical staff in field, this utility model can have various modifications and variations.All of the present utility model spirit and principle Within, any modification, equivalent substitution and improvement made etc., should be included within protection domain of the present utility model.

Claims (8)

1. a kind of isothermal method methanol converts the system of stable light hydrocarbon processed it is characterised in that described system includes material benzenemethanol supply Device, methanol gasifying superheater, reactor, steam generator, cooler and oil gas water separator, described material benzenemethanol supply The outlet of device connects to the feedstock input of described methanol gasifying superheater, the raw material delivery outlet of described methanol gasifying superheater Connect to the reacting material inlet of described reactor, the reacting material outlet of described reactor connects to described steam generator Thermal material import, the material outlet of described steam generator connects to the recuperation of heat import of described methanol gasifying superheater, institute The recuperation of heat outlet stating methanol gasifying superheater connects to described cooler, and described cooler is with described oil gas water separator even Logical.

2. isothermal method methanol according to claim 1 converts the system of stable light hydrocarbon processed it is characterised in that described methanol gas Change methanol gasifying device and the methanol superheater that superheater includes being independently arranged, the raw material first after described methanol gasifying device is processed Alcohol flows into described methanol superheater, and described raw material delivery outlet and described recuperation of heat import are respectively arranged at described methanol superheater On, described feedstock input and described recuperation of heat outlet be arranged on described methanol gasifying device.

3. isothermal method methanol according to claim 1 converts the system of stable light hydrocarbon processed it is characterised in that described reactor Including communicating with each other and the adiabatic pre-reactor that arranges independently of one another and isothermal reactor, the first thing of described thermal insulation pre-reactor Material import connects to the described raw material delivery outlet of described methanol gasifying superheater, and the first material outlet of described isothermal reactor is even It is connected to the described thermal material import of described steam generator.

4. isothermal method methanol according to claim 1 converts the system of stable light hydrocarbon processed it is characterised in that described reactor Including communicating with each other and the isothermal pre-reactor that arranges independently of one another and isothermal main reactor, the second of described isothermal pre-reactor Material inlet connects to the described raw material delivery outlet of described methanol gasifying superheater, and the second material of described isothermal main reactor goes out Mouth connects to the described thermal material import of described steam generator.

5. isothermal method methanol according to claim 1 converts the system of stable light hydrocarbon processed it is characterised in that described reactor Including for carrying out the isothermal pre-reaction room of isothermal pre-reaction section and for carrying out the isothermal main reaction chamber of isothermal primary response section, Described isothermal pre-reaction room and described isothermal main reaction chamber are arranged at the inside of described reactor and communicate with each other, described anti- The described reacting material inlet answering device is connected with described isothermal pre-reaction room, the described reacting material outlet of described reactor and institute State isothermal main reaction chamber to connect.

6. isothermal method methanol according to claim 1 converts the system of stable light hydrocarbon processed it is characterised in that described reactor Including the adiabatic pre-reaction room being arranged on described inside reactor and isothermal reaction room, and described thermal insulation pre-reaction room with described Isothermal reaction room communicates with each other, and the described reacting material inlet of described reactor is connected with described thermal insulation pre-reaction room, described anti- The described reacting material outlet answering device is connected with described isothermal reaction room.

7. isothermal method methanol according to claim 1 converts the system of stable light hydrocarbon processed it is characterised in that described reactor For isothermal reactor, described isothermal reactor includes beds side and cooling medium side.

8. isothermal method methanol according to claim 7 convert stable light hydrocarbon processed system it is characterised in that described system also Including cooling medium circulation device, described cooling medium circulation device is connected with the described cooling medium side of described isothermal reactor Connect.